Carbon dioxide electrolytic device and method of electrolyzing carbon dioxide

ABSTRACT

A carbon dioxide electrolytic device comprises: an electrolysis cell including a cathode, an anode, a carbon dioxide source to supply carbon dioxide to the cathode, a solution source to supply an electrolytic solution, and a separator separating the anode and the cathode; a power controller connected to the anode and the cathode; a refresh material source including a gas source to supply a gaseous substance, and a solution source to supply a rinse solution; and a controller to control the carbon dioxide source, the solution source, the power controller, and the refresh material source in accordance with request criteria of a performance of the cell and thus stop the supply of the carbon dioxide and the electrolytic solution, and apply the voltage therebetween while supplying the rinse solution thereto.

CROSS REFERENCE TO RELATED APPLICATION

This application is based upon and claims the benefit of priority from Japanese Patent Application No. 2017-180389, filed on Sep. 20, 2017; the entire contents of which are incorporated herein by reference.

FIELD

Embodiments described herein relate generally to a carbon dioxide electrolytic device and a method of electrolyzing carbon dioxide.

BACKGROUND

In recent years, depletion of fossil fuel such as petroleum or coal has been concerned, and expectation for sustainably-usable renewable energy has been rising. As the renewable energy, a solar cell, wind power generation, and the like can be cited. Because a power generation amount of these depends on weather and a natural situation, there is a problem that it is difficult to realize stable supply of electric power. For this reason, there has been made an attempt to store the electric power generated by the renewable energy in a storage battery, to thereby stabilize the electric power. However, when the electric power is stored, there are problems that a cost is required for the storage battery, and a loss occurs at a time of the storage.

With respect to such points, attention is focused on a technology in which water electrolysis is performed by using the electric power generated by the renewable energy to produce hydrogen (H₂) from water, or carbon dioxide (CO₂) is electrochemically reduced to be converted into a chemical substance (chemical energy) such as a carbon compound such as carbon monoxide (CO), formic acid (HCOOH), methanol (CH₃OH), methane (CH₄), acetic acid (CH₃COOH), ethanol (C₂H₅OH), ethane (C₂H₆), or ethylene (C₂H₄). When these chemical substances are stored in a cylinder or a tank, there are advantageous points that a storage cost of energy can be reduced, and a storage loss is also small, when compared to a case where the electric power (electric energy) is stored in the storage battery.

As a carbon dioxide electrolytic device, for example, a structure in which an Ag nanoparticle catalyst is used as a cathode, a cathode solution and CO₂ gas are brought into contact with the cathode, and an anode solution is brought into contact with an anode is being studied. As a concrete configuration of the electrolytic device, for example, there can be cited a configuration which includes a cathode solution flow path disposed along one surface of the cathode, a CO₂ gas flow path disposed along the other surface of the cathode, an anode solution flow path disposed along one surface of an anode, and a separator disposed between the cathode solution flow path and the anode solution flow path. When a reaction of producing, for example, CO from CO₂ is performed for a long period of time by using the electrolytic device having such a configuration and, for example, by making a constant current flow through the cathode and the anode, there is a problem that a deterioration over time of a cell performance such that a production amount of CO is reduced or a cell voltage is increased occurs. For this reason, there has been demanded a carbon dioxide electrolytic device capable of suppressing the deterioration over time of the cell performance.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a view illustrating a carbon dioxide electrolytic device of a first embodiment.

FIG. 2 is a sectional view illustrating an electrolysis cell of the carbon dioxide electrolytic device illustrated in FIG. 1.

FIG. 3 is a view illustrating one example of an anode solution flow path in the electrolysis cell illustrated in FIG. 2.

FIG. 4 is a view illustrating one example of a cathode solution flow path in the electrolysis cell illustrated in FIG. 2.

FIG. 5 is a view illustrating another example of the cathode solution flow path in the electrolysis cell illustrated in FIG. 2.

FIG. 6 is a view illustrating one example of a CO₂ gas flow path in the electrolysis cell illustrated in FIG. 2.

FIG. 7 is a view illustrating one example of a cathode in the electrolysis cell illustrated in FIG. 2.

FIG. 8 is a view illustrating another example of the cathode in the electrolysis cell illustrated in FIG. 2.

FIG. 9 is a view schematically illustrating a reaction in the cathode in the electrolysis cell illustrated in FIG. 2.

FIG. 10 is a chart illustrating an operation step of the carbon dioxide electrolytic device of the first embodiment.

FIG. 11 is a chart illustrating a refresh step of the carbon dioxide electrolytic device of the first embodiment.

FIG. 12 is a view illustrating a carbon dioxide electrolytic device of a second embodiment.

FIG. 13 is a sectional view illustrating an electrolysis cell of the carbon dioxide electrolytic device illustrated in FIG. 12.

FIG. 14 is a view illustrating a carbon dioxide electrolytic device of a third embodiment.

FIG. 15 is a sectional view illustrating an electrolysis cell of the carbon dioxide electrolytic device illustrated in FIG. 14.

DETAILED DESCRIPTION

A carbon dioxide electrolytic device, comprising: an electrolysis cell including a cathode to reduce carbon dioxide and thus produce a carbon compound, an anode to oxidize water or hydroxide ions and thus produce oxygen, a carbon dioxide source to supply carbon dioxide to the cathode, a solution source to supply an electrolytic solution containing water to at least one selected from the group consisting of the cathode and the anode, and a separator separating the anode and the cathode; a power controller connected to the anode and the cathode and configured to apply a voltage therebetween; a refresh material source including a gas source to supply a gaseous substance to at least one selected from the group consisting of the anode and the cathode, and a solution supply source to supply a rinse solution to at least one selected from the group consisting of the anode and the cathode; and a controller to control the carbon dioxide source, the solution source, the power controller, and the refresh material source in accordance with request criteria of a performance of the cell and thus stop the supply of the carbon dioxide and the electrolytic solution, and apply the voltage therebetween while supplying the rinse solution thereto.

Hereinafter, a carbon dioxide electrolytic device of an embodiment will be described with reference to the drawings. In each embodiment presented below, substantially the same components are denoted by the same reference signs, and a description thereof is sometimes partially omitted. The drawings are schematic, and a relationship between a thickness and a planar size, thickness proportions of the respective portions, and the like are sometimes different from actual ones.

First Embodiment

FIG. 1 is a view illustrating a configuration of a carbon dioxide electrolytic device according to a first embodiment, and FIG. 2 is a sectional view illustrating a configuration of an electrolysis cell in the electrolytic device illustrated in FIG. 1. A carbon dioxide electrolytic device 1 illustrated in FIG. 1 includes an electrolysis cell 2, an anode solution supply system 100 which supplies an anode solution to the electrolysis cell 2, a cathode solution supply system 200 which supplies a cathode solution to the electrolysis cell 2, a gas supply system 300 which supplies carbon dioxide (CO₂) gas to the electrolysis cell 2, a product collection system 400 which collects a product produced by a reduction reaction in the electrolysis cell 2, a control system 500 which detects a type and a production amount of the collected product, and performs control of the product and control of a refresh operation, a waste solution collection system 600 which collects a waste solution of the cathode solution and the anode solution, and a refresh material source 700 which recovers an anode, a cathode, or the like of the electrolysis cell 2.

As illustrated in FIG. 2, the electrolysis cell 2 includes an anode part 10, a cathode part 20, and a separator 30. The anode part 10 includes an anode 11, an anode solution flow path 12, and an anode current collector 13. The cathode part 20 includes a cathode solution flow path 21, a cathode 22, a CO₂ gas flow path 23, and a cathode current collector 24. The separator 30 is disposed to separate the anode part 10 and the cathode part 20. The electrolysis cell 2 is sandwiched by a pair of support plates, which are not illustrated, and further tightened by bolts or the like. In FIG. 1 and FIG. 2, there is provided a power controller 40 which makes a current flow through the anode 11 and the cathode 22. The power controller 40 is connected to the anode 11 and the cathode 22 via a current introduction member. The power controller 40 is not limited to a normal system power supply, battery, or the like, and may be one having a power source which supplies electric power generated by renewable energy such as a solar cell or wind power generation. Note that the power controller 40 may also have the aforementioned power source and a power controller or the like that adjusts an output of the aforementioned power source to control a voltage between the anode 11 and the cathode 22.

The anode 11 is an electrode (oxidation electrode) which causes an oxidation reaction of water (H₂O) in an anode solution as an electrolytic solution to produce oxygen (O₂) or hydrogen ions (H⁺), or causes an oxidation reaction of hydroxide ions (OH⁻) produced in the cathode part 20 to produce oxygen (O₂) or water (H₂O). The anode 11 preferably has a first surface 11 a which is brought into contact with the separator 30, and a second surface 11 b which faces the anode solution flow path 12. The first surface 11 a of the anode 11 is brought into close contact with the separator 30. The anode solution flow path 12 supplies the anode solution to the anode 11, and is formed of a pit (groove portion/concave portion) provided in a first flow path plate 14. The anode solution flows through inside the anode solution flow path 12 so as to be brought into contact with the anode 11. The anode current collector 13 is electrically brought into contact with a surface on a side opposite to the anode 11 of the first flow path plate 14 which forms the anode solution flow path 12.

As described above, in the electrolysis cell 2 of the embodiment, the anode 11 and the separator 30 are brought into close contact with each other. In the anode 11, oxygen (O₂) is produced, and at this time, in a cell structure in which a separator is sandwiched by a cathode solution flow path and an anode solution flow path, air bubbles of oxygen (O₂) gas generated in the anode 11 stay in the anode solution flow path, and a cell resistance between the anode and the separator (ion exchange membrane or the like) increases, this sometimes increases a voltage variation of the anode. With respect to a point as above, the anode solution flow path 12 is not disposed between the anode 11 and the separator 30, and by making the anode 11 and the separator 30 to be brought into close contact with each other, oxygen gas generated in the anode 11 is discharged to the anode solution flow path 12 together with the anode solution. This makes it possible to prevent the oxygen gas from staying between the anode 11 and the separator 30, and it becomes possible to suppress a variation in a cell voltage due to the voltage variation of the anode.

To the first flow path plate 14, there are provided a solution inlet port and a solution outlet port whose illustrations are omitted, and the anode solution is introduced and discharged by the anode solution supply system 100 via these solution inlet port and solution outlet port. It is preferable to use a material having low chemical reactivity and high conductivity for the first flow path plate 14. As such a material, there can be cited a metal material such as Ti or SUS, carbon, or the like. It is preferable that the anode solution flow path 12 is provided with a plurality of lands (convex portions) 15, as illustrated in FIG. 3. The lands 15 are provided for mechanical retention and electrical continuity. The lands 15 are preferably provided in an alternate manner for uniformizing the flow of the anode solution. Since the lands 15 as above are provided, the anode solution flow path 12 meanders. In addition, also for the purpose of realizing good discharge of the anode solution containing oxygen (O₂) gas mixed therein, it is preferable that the lands 15 are provided in an alternate manner to the anode solution flow path 12 to make the anode solution flow path 12 meander.

It is preferable that the anode 11 is mainly constituted of a catalyst material (anode catalyst material) capable of oxidizing water (H₂O) to produce oxygen or hydrogen ions or oxidizing hydroxide ions (OH⁻) to produce water or oxygen, and capable of reducing an overvoltage in such a reaction. As such a catalyst material, there can be cited a metal such as platinum (Pt), palladium (Pd), or nickel (Ni), an alloy or an intermetallic compound containing the above metals, a binary metal oxide such as a manganese oxide (Mn—O), an iridium oxide (Ir—O), a nickel oxide (Ni—O), a cobalt oxide (Co—O), an iron oxide (Fe—O), a tin oxide (Sn—O), an indium oxide (In—O), a ruthenium oxide (Ru—O), a lithium oxide (Li—O), or a lanthanum oxide (La—O), a ternary metal oxide such as Ni—Co—O, Ni—Fe—O, La—Co—O, Ni—La—O, or Sr—Fe—O, a quaternary metal oxide such as Pb—Ru—Ir—O or La—Sr—Co—O, or a metal complex such as a Ru complex or an Fe complex.

The anode 11 includes a base material having a structure capable of making the anode solution or ions move between the separator 30 and the anode solution flow path 12, for example, a porous structure such as a mesh material, a punching material, a porous body, or a metal fiber sintered body. The base material may be constituted of a metal such as titanium (Ti), nickel (Ni), or iron (Fe), or a metal material such as an alloy (for example, SUS) containing at least one of these metals, or may be constituted of the above-described anode catalyst material. When an oxide is used as the anode catalyst material, it is preferable to form a catalyst layer in a manner that the anode catalyst material is adhered to or stacked on a surface of the base material made of the above-described metal material. The anode catalyst material preferably has nanoparticles, a nanostructure, a nanowire, or the like for the purpose of increasing the oxidation reaction. The nanostructure is a structure in which nanoscale irregularities are formed on a surface of the catalyst material.

The cathode 22 is an electrode (reduction electrode) which causes a reduction reaction of carbon dioxide (CO₂) or a reduction reaction of a carbon compound produced thereby to produce a carbon compound such as carbon monoxide (CO), methane (CH₄), ethane (C₂H₆), ethylene (C₂H₄), methanol (CH₃OH), ethanol (C₂H₅OH), or ethylene glycol (C₂H₆O₂). In the cathode 22, there is a case where a side reaction in which hydrogen (H₂) is produced by a reduction reaction of water (H₂O) is caused simultaneously with the reduction reaction of carbon dioxide (CO₂). The cathode 22 has a first surface 22 a facing the cathode solution flow path 21, and a second surface 22 b facing the CO₂ gas flow path 23. The cathode solution flow path 21 is disposed between the cathode 22 and the separator 30 so that the cathode solution as an electrolytic solution is brought into contact with the cathode 22 and the separator 30.

The cathode solution flow path 21 is formed of an opening portion provided in a second flow path plate 25. To the second flow path plate 25, there are provided a solution inlet port and a solution outlet port whose illustrations are omitted, and the cathode solution is introduced and discharged by the cathode solution supply system 200 via these solution inlet port and solution outlet port. The cathode solution flows through inside the cathode solution flow path 21 so as to be brought into contact with the cathode 22 and the separator 30. It is preferable to use a material having low chemical reactivity and having no conductivity for the second flow path plate 25 forming the cathode solution flow path 21. As such a material, there can be cited an insulating resin material such as an acrylic resin, polyetheretherketone (PEEK), or a fluorocarbon resin.

In the cathode 22, the reduction reaction of CO₂ occurs mainly in a portion which is brought into contact with the cathode solution. For this reason, it is preferable to apply an opening portion with a wide opening area to the cathode solution flow path 21, as illustrated in FIG. 4. However, in order to increase the mechanical retention and the electrical connectivity, it is also possible to provide a land (convex portion) 26 to the cathode solution flow path 21, as illustrated in FIG. 5. The land 26 of the cathode solution flow path 21 is provided at a center portion of the cathode solution flow path 21, and is retained to the second flow path plate 25 by a bridge portion 27 which is thinner than the land 26, in order not to prevent the flow of the cathode solution in the cathode solution flow path 21. When the land 26 is provided to the cathode solution flow path 21, the number of lands 26 is preferably small in order to reduce a cell resistance.

The CO₂ gas flow path 23 is formed of a pit (groove portion/concave portion) provided in a third flow path plate 28. It is preferable to use a material having low chemical reactivity and high conductivity for the third flow path plate 28 forming the CO₂ gas flow path. As such a material, there can be cited a metal material such as Ti or SUS, carbon, or the like. Note that in each of the first flow path plate 14, the second flow path plate 25, and the third flow path plate 28, an inlet port and an outlet port for a solution or gas, screw holes for tightening, and the like, whose illustrations are omitted, are provided. Further, in front of and behind each of the flow path plates 14, 25, and 28, packing whose illustration is omitted is sandwiched according to need.

To the third flow path plate 28, a gas inlet port and a gas outlet port whose illustrations are omitted are provided, and CO₂ gas or gas containing CO₂ (sometimes collectively referred to simply as CO₂ gas) is introduced and discharged by the gas supply system 300 via these gas inlet port and gas outlet port. The CO₂ gas flows through inside the CO₂ gas flow path 23 so as to be brought into contact with the cathode 22. It is preferable that the CO₂ gas flow path 23 is provided with a plurality of lands (convex portions) 29, as illustrated in FIG. 6. The lands 29 are provided for mechanical retention and electrical continuity. The lands 29 are preferably provided in an alternate manner, which realizes a state where the CO₂ gas flow path 23 meanders similarly to the anode solution flow path 12. The cathode current collector 24 is electrically brought into contact with a surface on a side opposite to the cathode 22 of the third flow path plate 28.

In the electrolysis cell 2 of the embodiment, by providing the lands 15 and 29 to the anode solution flow path 12 and the CO₂ gas flow path 23, it is possible to increase a contact area between the anode 11 and the first flow path plate 14 forming the anode solution flow path 12, and a contact area between the cathode 22 and the third flow path plate 28 forming the CO₂ gas flow path 23. Further, by providing the land 26 to the cathode solution flow path 21, it is possible to increase a contact area between the cathode 22 and the second flow path plate 25 forming the cathode solution flow path 21. These realize good electrical continuity between the anode current collector 13 and the cathode current collector 24 while enhancing mechanical retentivity of the electrolysis cell 2, and it becomes possible to improve reduction reaction efficiency of CO₂, and the like.

As illustrated in FIG. 7, the cathode 22 has a gas diffusion layer 22A and a cathode catalyst layer 22B provided on the gas diffusion layer 22A. As illustrated in FIG. 8, it is also possible that a porous layer 22C denser than the gas diffusion layer 22A is disposed between the gas diffusion layer 22A and the cathode catalyst layer 22B. As illustrated in FIG. 9, the gas diffusion layer 22A is disposed on the CO₂ gas flow path 23 side, and the cathode catalyst layer 22B is disposed on the cathode solution flow path 21 side. The cathode catalyst layer 22B may enter the gas diffusion layer 22A. The cathode catalyst layer 22B preferably has catalyst nanoparticles, a catalyst nanostructure, or the like. The gas diffusion layer 22A is constituted of, for example, carbon paper, carbon cloth, or the like, and water repellent treatment is performed thereon. The porous layer 22C is constituted of a porous body whose pore size is smaller than that of the carbon paper or the carbon cloth.

As illustrated in a schematic view in FIG. 9, in the cathode catalyst layer 22B, the cathode solution or ions are supplied and discharged from the cathode solution flow path 21. In the gas diffusion layer 22A, the CO₂ gas is supplied from the CO₂ gas flow path 23, and a product obtained by the reduction reaction of the CO₂ gas is discharged. By previously performing moderate water repellent treatment on the gas diffusion layer 22A, the CO₂ gas reaches the cathode catalyst layer 22B mainly through gas diffusion. The reduction reaction of CO₂ or the reduction reaction of a carbon compound produced thereby occurs in the vicinity of a boundary between the gas diffusion layer 22A and the cathode catalyst layer 22B or in the vicinity of the cathode catalyst layer 22B which enters the gas diffusion layer 22A, a gaseous product is discharged mainly from the CO₂ gas flow path 23, and a liquid product is discharged mainly from the cathode solution flow path 21.

The cathode catalyst layer 22B is preferably constituted of a catalyst material (cathode catalyst material) capable of reducing carbon dioxide to produce a carbon compound, capable of reducing the carbon compound produced thereby to produce a carbon compound according to need, and capable of reducing an overvoltage in the above reaction. As such a material, there can be cited a metal such as gold (Au), silver (Ag), copper (Cu), platinum (Pt), palladium (Pd), nickel (Ni), cobalt (Co), iron (Fe), manganese (Mn), titanium (Ti), cadmium (Cd), zinc (Zn), indium (In), gallium (Ga), lead (Pb), or tin (Sn), a metal material such as an alloy or an intermetallic compound containing at least one of the above metals, a carbon material such as carbon (C), graphene, CNT (carbon nanotube), fullerene, or ketjen black, or a metal complex such as a Ru complex or a Re complex. The cathode catalyst layer 22B can employ various shapes such as a plate shape, a mesh shape, a wire shape, a particle shape, a porous shape, a thin film shape, and an island shape.

The cathode catalyst material constituting the cathode catalyst layer 22B preferably has nanoparticles of the above-described metal material, a nanostructure of the metal material, a nanowire of the metal material, or a composite body in which the nanoparticles of the above-described metal material are supported by a carbon material such as carbon particles, a carbon nanotube, or graphene. By applying catalyst nanoparticles, a catalyst nanostructure, a catalyst nanowire, a catalyst nano-support structure, or the like as the cathode catalyst material, it is possible to increase reaction efficiency of the reduction reaction of carbon dioxide in the cathode 22.

The separator 30 is constituted of an ion exchange membrane or the like capable of making ions move between the anode 11 and the cathode 22, and capable of separating the anode part 10 and the cathode part 20. As the ion exchange membrane, it is possible to use, for example, a cation exchange membrane such as Nafion or Flemion, or an anion exchange membrane such as Neosepta or Selemion. As will be described later, when an alkaline solution is used as the anode solution and the cathode solution, and it is assumed that hydroxide ions (OH⁻) move mainly, the separator 30 is preferably constituted of the anion exchange membrane. However, other than the ion exchange membrane, it is also possible to apply a glass filter, a porous polymeric membrane, a porous insulating material, or the like to the separator 30, as long as they are a material capable of making ions move between the anode 11 and the cathode 22.

Each of the anode solution and the cathode solution as the electrolytic solution is preferably a solution containing at least water (H₂O). Because carbon dioxide (CO₂) is supplied from the CO₂ gas flow path 23, the cathode solution may contain or need not contain carbon dioxide (CO₂). To the anode solution and the cathode solution, the same solution may be applied or different solutions may be applied. As a solution containing H₂O used as the anode solution and the cathode solution, an aqueous solution containing an arbitrary electrolyte can be cited. As the aqueous solution containing the electrolyte, there can be cited, for example, an aqueous solution containing at least one selected from a hydroxide ion (OH⁻), a hydrogen ion (H⁺), a potassium ion (K⁺), a sodium ion (Na⁺), a lithium ion (Li⁺), a chloride ion (Cl⁻), a bromide ion (Br⁻), an iodide ion (I⁻), a nitrate ion (NO₃ ⁻), a sulfate ion (SO₄ ²⁻), a phosphate ion (PO₄ ²⁻), a borate ion (BO₃ ³⁻), and a hydrogen carbonate ion (HCO₃ ⁻). In order to reduce an electrical resistance of the electrolytic solution, it is preferable to use, as the anode solution and the cathode solution, an alkaline solution in which an electrolyte such as a potassium hydroxide or a sodium hydroxide is dissolved in high concentration.

For the cathode solution, it is also possible to use an ionic liquid which is made of salts of cations such as imidazolium ions or pyridinium ions and anions such as BF₄ ⁻ or PF₆ ⁻ and which is in a liquid state in a wide temperature range, or its aqueous solution. As another cathode solution, there can be cited an amine solution of ethanolamine, imidazole, pyridine, or the like, or an aqueous solution thereof. As amine, any of primary amine, secondary amine, and tertiary amine is applicable.

To the anode solution flow path 12 of the anode part 10, the anode solution is supplied from the anode solution supply system 100. The anode solution supply system 100 circulates the anode solution so that the anode solution flows through inside the anode solution flow path 12. The anode solution supply system 100 has a pressure controller 101, an anode solution tank 102, a flow rate controller (pump) 103, a reference electrode 104, and a pressure gauge 105, and is configured to make the anode solution circulate in the anode solution flow path 12. The anode solution tank 102 is connected to a not-illustrated gas component collection unit which collects a gas component such as oxygen (O₂) contained in the circulating anode solution. The anode solution is introduced into the anode solution flow path 12 after a flow rate and a pressure thereof are controlled in the pressure controller 101 and the flow rate controller 103.

To the cathode solution flow path 21 of the cathode part 20, the cathode solution is supplied from the cathode solution supply system 200. The cathode solution supply system 200 circulates the cathode solution so that the cathode solution flows through inside the cathode solution flow path 21. The cathode solution supply system 200 has a pressure controller 201, a cathode solution tank 202, a flow rate controller (pump) 203, a reference electrode 204, and a pressure gauge 205, and is configured to make the cathode solution circulate in the cathode solution flow path 21. The cathode solution tank 202 is connected to a gas component collection unit 206 which collects a gas component such as carbon monoxide (CO) contained in the circulating cathode solution. The cathode solution is introduced into the cathode solution flow path 21 after a flow rate and a pressure thereof are controlled in the pressure controller 201 and the flow rate controller 203.

To the CO₂ gas flow path 23, the CO₂ gas is supplied from the gas supply system 300. The gas supply system 300 has a CO₂ gas cylinder 301, a flow rate controller 302, a pressure gauge 303, and a pressure controller 304. The CO₂ gas is introduced into the CO₂ gas flow path 23 after a flow rate and a pressure thereof are controlled in the flow rate controller 302 and the pressure controller 304. The gas supply system 300 is connected to the product collection system 400 which collects a product in the gas flowed through the CO₂ gas flow path 23. The product collection system 400 has a gas/liquid separation unit 401 and a product collection unit 402. A reduction product such as CO or H₂ contained in the gas flowed through the CO₂ gas flow path 23 is accumulated in the product collection unit 402 via the gas/liquid separation unit 401.

The anode solution and the cathode solution circulate in the anode solution flow path 12 and the cathode solution flow path 21 at a time of an electrolytic reaction operation, as described above. At a time of a refresh operation of the electrolysis cell 2 to be described later, the anode solution and the cathode solution are discharged to the waste solution collection system 600 so that the anode 11, the anode solution flow path 12, the cathode 22, the cathode solution flow path 21, and the like are exposed from the anode solution and the cathode solution. The waste solution collection system 600 has a waste solution collection tank 601 connected to the anode solution flow path 12 and the cathode solution flow path 21. Waste solutions of the anode solution and the cathode solution are collected in the waste solution collection tank 601 by opening and closing not-illustrated valves. The opening and closing of the valves, or the like is controlled collectively by the control system 500. The waste solution collection tank 601 also functions as a collection unit of a rinse solution supplied from the refresh material source 700. Further, a gaseous substance supplied from the refresh material source 700 and containing a part of a liquid substance, is also collected by the waste solution collection tank 601 according to need.

The refresh material source 700 includes a gaseous substance supply system 710 and a rinse solution supply system 720. Note that the rinse solution supply system 720 can be omitted according to circumstances. The gaseous substance supply system 710 has a gas tank 711 to be a supply source of a gaseous substance such as air, carbon dioxide, oxygen, nitrogen, or argon, and a pressure controller 712 which controls a supply pressure of the gaseous substance. The rinse solution supply system 720 has a rinse solution tank 721 to be a supply source of a rinse solution such as water and a flow rate controller (pump) 722 which controls a supply flow rate or the like of the rinse solution. The gaseous substance supply system 710 and the rinse solution supply system 720 are connected to the anode solution flow path 12, the cathode solution flow path 21, and the CO₂ gas flow path 23 via pipes. The gaseous substance and the rinse solution are supplied to each of the flow paths 12, 21, and 23 by opening and closing not-illustrated valves. The opening and closing of the valves, or the like is controlled collectively by the control system 500.

A part of the reduction product accumulated in the product collection unit 402 is sent to a reduction performance detection unit 501 of the control system 500. In the reduction performance detection unit 501, a production amount and a proportion of each product such as CO or H₂ in the reduction product, are detected. The detected production amount and proportion of each product are input into a data collection and controller 502 of the control system 500. Further, the data collection and controller 502 collects electrical data such as a cell voltage, a cell current, a cathode potential, and an anode potential, pressures and pressure losses inside the anode solution flow path and the cathode solution flow path as part of a cell performance of the electrolysis cell 2, and transmits the data to a refresh controller 503.

The data collection and controller 502 is electrically connected, via bi-directional signal lines whose illustration is partially omitted, to the power controller 40, the pressure controller 101 and the flow rate controller 103 of the anode solution supply system 100, the pressure controller 201 and the flow rate controller 203 of the cathode solution supply system 200, the flow rate controller 302 and the pressure controller 304 of the gas supply system 300, and the pressure controller 712 and the flow rate controller 722 of the refresh material source 700, in addition to the reduction performance detection unit 501, and these are collectively controlled. Note that each pipe is provided with a not-illustrated valve, and an opening/closing operation of the valve is controlled by a signal from the data collection and controller 502. The data collection and controller 502 may also control operations of the aforementioned components at a time of an electrolysis operation, for example.

The refresh controller 503 is electrically connected, via bi-directional signal lines whose illustration is partially omitted, to the power controller 40, the flow rate controller 103 of the anode solution supply system 100, the flow rate controller 203 of the cathode solution supply system 200, the flow rate controller 302 of the gas supply system 300, and the pressure controller 712 and the flow rate controller 722 of the refresh material source 700, and these are collectively controlled. Note that each pipe is provided with a not-illustrated valve, and an opening/closing operation of the valve is controlled by a signal from the refresh controller 503. The refresh controller 503 may also control operations of the aforementioned components at a time of the electrolysis operation, for example. Further, it is also possible that the refresh controller 503 and the data collection and controller 502 are configured by one controller.

A working operation of the carbon dioxide electrolytic device 1 of the embodiment will be described. First, as illustrated in FIG. 10, a start-up step S101 of the electrolytic device 1 is performed. In the start-up step S101 of the electrolytic device 1, the following operation is performed. In the anode solution supply system 100, a flow rate and a pressure are controlled by the pressure controller 101 and the flow rate controller 103, and the anode solution is introduced into the anode solution flow path 12. In the cathode solution supply system 200, a flow rate and a pressure are controlled by the pressure controller 201 and the flow rate controller 203, and the cathode solution is introduced into the cathode solution flow path 21. In the gas supply system 300, a flow rate and a pressure are controlled by the flow rate controller 302 and the pressure controller 304, and CO₂ gas is introduced into the CO₂ gas flow path 23.

Next, a CO₂ electrolysis operation step S102 is performed. In the CO₂ electrolysis operation step S102, application of an electrolytic voltage is started by the power controller 40 of the electrolytic device 1 after being subjected to the start-up step S101, and a current is supplied by applying the voltage between the anode 11 and the cathode 22. When the current is made to flow between the anode 11 and the cathode 22, an oxidation reaction in the vicinity of the anode 11 and a reduction reaction in the vicinity of the cathode 22 occur, which will be described below. Here, a case of producing carbon monoxide (CO) as the carbon compound is mainly described, but, the carbon compound as the reduction product of carbon dioxide is not limited to carbon monoxide, and may be other carbon compounds such as the above-described organic compounds. Further, as a reaction process caused by the electrolysis cell 2, there can be considered a case where hydrogen ions (H⁺) are mainly produced and a case where hydroxide ions (OH⁻) are mainly produced, but, it is not limited to either of these reaction processes.

First, the reaction process in a case of mainly oxidizing water (H₂O) to produce hydrogen ions (H⁺) is described. When a current is supplied between the anode 11 and the cathode 22 from the power controller 40, an oxidation reaction of water (H₂O) occurs in the anode 11 which is brought into contact with the anode solution. Concretely, as presented in the following formula (1), H₂O contained in the anode solution is oxidized, and oxygen (O₂) and hydrogen ions (H⁺) are produced.

2H₂O→4H⁺+O₂+4e ⁻  (1)

H⁺ produced in the anode 11 moves in the anode solution existing in the anode 11, the separator 30, and the cathode solution in the cathode solution flow path 21, and reaches the vicinity of the cathode 22. The reduction reaction of carbon dioxide (CO₂) occurs by electrons (e) based on the current supplied from the power controller 40 to the cathode 22 and H⁺ moved to the vicinity of the cathode 22. Concretely, as presented in the following formula (2), CO₂ supplied from the CO₂ gas flow path 23 to the cathode 22 is reduced, and CO is produced.

2CO₂+4H⁺+4e ⁻→2CO+2H₂O  (2)

Next, the reaction process in a case of mainly reducing carbon dioxide (CO₂) to produce hydroxide ions (OH⁻) is described. When a current is supplied between the anode 11 and the cathode 22 from the power controller 40, in the vicinity of the cathode 22, water (H₂O) and carbon dioxide (CO₂) are reduced, and carbon monoxide (CO) and hydroxide ions (OH⁻) are produced, as presented in the following formula (3). The hydroxide ions (OH⁻) diffuse to the vicinity of the anode 11, and as presented in the following formula (4), the hydroxide ions (OH⁻) are oxidized, and oxygen (O₂) is produced.

2CO₂+2H₂O+4e ⁻→2CO+4OH⁻  (3)

4OH⁻→2H₂O+O₂+4e ⁻  (4)

In the above-described reaction processes in the cathode 22, the reduction reaction of CO₂ is considered to occur in the vicinity of the boundary between the gas diffusion layer 22A and the cathode catalyst layer 22B, as described above. At this time, the cathode solution which flows through the cathode solution flow path 21 enters up to the gas diffusion layer 22A or the cathode catalyst layer 22B has excess water, which causes a trouble such that the production amount of CO obtained by the reduction reaction of CO₂ reduces or the cell voltage increases. The reduction in the cell performance of the electrolysis cell 2 as above is also caused by not only deviation of distribution of ions and residual gas in the vicinity of the anode 11 and the cathode 22, the excess water in the cathode catalyst layer 22B, and precipitation of an electrolyte in the cathode 22 and the anode 11, but also precipitation of an electrolyte in the anode solution flow path 12 and the cathode solution flow path 21, and the like.

Further, there is a case where the electrolysis operation causes precipitation of salts in the cathode solution flow path 21 or the gas diffusion layer 22A, which blocks the flow path or reduces the gas diffusibility, resulting in that the cell performance reduces. This is because ions move between the anode 11 and the cathode 22 via the separator 30 or the ion exchange membrane, and the ions react with the gas component. For example, when a potassium hydroxide solution is used as the anode solution, and carbon dioxide gas is used as the cathode gas, potassium ions move from the anode 11 to the cathode 22, and the ions react with carbon dioxide to produce salts of potassium hydroxide, potassium carbonate, or the like. In the cathode solution flow path 21 or the gas diffusion layer 22A, when an amount of the salts is equal to or less than the solubility, the salts precipitate in the cathode solution flow path 21 or the gas diffusion layer 22A. When the flow path is blocked, a uniform gas flow in the entire cell is prevented, and the cell performance lowers. In particular, when a plurality of cathode solution flow paths 21 are provided, the cell performance significantly lowers. Note that there is a case where the performance of the cell itself is improved by partial increase in the gas flow rate and the like. This is because since a gas pressure is increased, the gas component or the like supplied to the catalyst increases or the gas diffusibility increases, which improves the cell performance. In order to detect the reduction in the cell performance as above, a step S103 which determines whether or not the cell performance satisfies the request criteria, is performed.

The data collection and controller 502 collects the production amount and the proportion of each product and the cell performance such as the cell voltage, the cell current, the cathode potential, the anode potential, the pressure inside the anode solution flow path 12, the pressure inside the cathode solution flow path 21 in the electrolysis cell 2 regularly or continuously, for example, as described above. Further, in the data collection and controller 502, the request criteria of the cell performance are previously set, and it is determined whether or not collected data satisfies the set request criteria. When the collected data satisfies the set request criteria, the CO₂ electrolysis operation S102 is continued without performing a CO₂ electrolysis stop (S104). When the collected data does not satisfy the set request criteria, a refresh operation step S105 is performed.

The cell performance collected by the data collection and controller 502 is defined by parameters such as an upper limit value of a cell voltage when a constant current is made to flow through the electrolysis cell 2, a lower limit value of a cell current when a constant voltage is applied to the electrolysis cell 2, and Faradaic efficiency of the carbon compound produced by the reduction reaction of CO₂. Here, the Faradaic efficiency is defined as a proportion of a current contributing to production of an intended carbon compound with respect to an entire current flowed through the electrolysis cell 2. In order to maintain electrolysis efficiency, the refresh operation step S105 may be performed when the upper limit value of the cell voltage when the constant current is made to flow reaches 150% or more, preferably 120% or more of a set value. Further, the refresh operation step S105 may be performed when the lower limit value of the cell current at a time of applying the constant voltage reaches 50% or less, preferably 80% or less of a set value. In order to maintain a production amount of the reduction product such as the carbon compound, the refresh operation step S105 may be performed when the Faradaic efficiency of the carbon compound becomes 50% or less, preferably 80% or less of a set value.

Regarding the determination of the cell performance, for example, when at least one parameter of the cell voltage, the cell current, the Faradaic efficiency of the carbon compound, the pressure inside the anode solution flow path 12, and the pressure inside the cathode solution flow path 21 does not satisfy the request criteria, it is determined that the cell performance does not satisfy the request criteria, and the refresh operation step S105 is carried out. Further, it is also possible to set the request criteria of the cell performance by combining two or more of the aforementioned parameters. For example, it is also possible to perform the refresh operation step S105 when neither the cell voltage nor the Faradaic efficiency of the carbon compound satisfies the request criteria. The refresh operation step S105 is performed when at least one of the cell performance does not satisfy the request criteria. In order to stably perform the CO₂ electrolysis operation step S102, the refresh operation step S105 is preferably performed at an interval of one hour or more, for example.

If the request criteria of the cell performance are judged based on only one of the cell voltage, the cell current, and the Faradaic efficiency of the carbon compound, when, even in a case where the cell performance improves or does not change, salts precipitate in the flow path or the gas diffusion layer to reduce the output, it is sometimes judged that the refresh is not required. In the electrolytic device, it is important to suspect the reduction in the cell performance beforehand, and to perform the refresh operation at an optimum timing. Accordingly, in the electrolytic device of the embodiment, it is preferable that the pressure in the cell (the pressure inside the anode solution flow path 12, the pressure inside the cathode solution flow path 21, or the like) is set to one of the parameters for defining the request criteria, to thereby sense the precipitation of salts, and the refresh operation is performed.

The judgment regarding the necessity of the refresh operation is made based on not only the cell voltage, the current value, and the sensing of salts based on a voltage change in the cell, but also the performance of gas/liquid separation between the anode 11 and the cathode 22 when the anode 11 and the cathode 22 are separated by the separator 30, namely, a movement amount of the liquid or the gas between the anode 11 and the cathode 22, an amount of the product, a voltage difference relative to a reference electrode, an estimated value of the Faradaic efficiency from these parameters, and the like. The Faradaic efficiency from the respective parameter values and the necessity of the refresh operation can be comprehensively determined as judgment of the necessity of the refresh operation also from parameters to be described later, and any combination of respective values and any calculation method are applicable.

It is also possible to judge the necessity of the refresh operation based on a flooding degree estimated from respective pieces of cell data, a voltage change, and the like based on an operating method for detecting a flooding performance. Further, it is also possible to take an operating time of the electrolysis cell 2 into consideration. The operating time is not limited to an operating time after the operation is started, but may be an integrated value of the operating time so far, a duration, an operating time after the refresh operation, a calculated value of multiplication between the integrated voltage value and time, or between the current value and the time, or the like, and any combination and calculation method thereof can be applied. Further, the calculated values of these combinations are preferable when compared to the judgment based on simply the duration or the like, since a difference caused by the operating method of the electrolysis cell 2 is taken into consideration. Furthermore, it is also possible to use a variation value of the current or the voltage, a pH value and a change value of the electrolytic solution, oxygen generation amount and variation amount.

It is preferable that the operation of judging the necessity of the refresh operation is performed, and the judgment is made based on the parameter such as a cell voltage at a time of the operation, since it is possible to accurately judge the necessity of the refresh operation, although the working operation time is reduced. Note that a judgment time of the necessity of the refresh operation in this case is preferably at least half a refresh operation time, more preferably ¼ or less of the refresh operation time, and ideally 1/10 or less of the refresh operation time. Further, regarding the respective parameters for judging the necessity of the refresh operation, respective pieces of data of the electrolysis cell 2 are collected via an electronic network, required parameters are derived by the data collection and controllers 502 and analysis units 504 of a plurality of cells, through big data analysis, and analysis of machine learning or the like, the refresh controller 503 is made to update the request criteria of the cell performance defined by the respective parameters for judging the necessity of refresh, and in a manner as above, it is possible to constantly perform the best refresh operation.

The refresh operation step S105 is performed according to a flow chart illustrated in FIG. 11, for example. First, the application of the electrolytic voltage performed by the power controller 40 is stopped, to thereby stop the reduction reaction of CO₂ (S201). At this time, the application of the electrolytic voltage does not necessarily have to be stopped. Next, the cathode solution and the anode solution are discharged from the cathode solution flow path 21 and the anode solution flow path 12 (S202). Next, the rinse solution is supplied to the cathode solution flow path 21 and the anode solution flow path 12 (S203), to thereby perform washing. While the rinse solution is supplied, a refresh voltage is applied between the anode 11 and the cathode 22. This makes it possible to remove ions and impurities adhered to the cathode catalyst layer 22B. When the refresh voltage is applied so as to perform mainly oxidation treatment, ions and impurities such as organic matters adhered to the surface of the catalyst are oxidized to be removed. Further, by performing this treatment in the rinse solution, it is possible to perform not only the refresh of the catalyst but also removal of ions substituted in an ion-exchange resin at a time of using the ion exchange membrane as the separator 30.

The refresh voltage is preferably not less than −2.5 V nor more than 2.5 V, for example. Since energy is used for the refresh operation, the range of the refresh voltage is preferably as narrow as possible, and the range is more preferably not less than −1.5 V nor more than 1.5 V, for example. The refresh voltage may be cyclically applied so that the oxidation treatment of the ions and the impurities and the reduction treatment are alternately performed. This makes it possible to accelerate regeneration of the ion-exchange resin and regeneration of the catalyst. Further, it is also possible to perform the refresh operation by applying, as the refresh voltage, a voltage whose value is equal to that of the electrolytic voltage at a time of the electrolysis operation. In this case, it is possible to simplify the configuration of the power controller 40.

Next, gas is supplied to the cathode solution flow path 21 and the anode solution flow path 12 (S204), to thereby dry the cathode 22 and the anode 11. When the rinse solution is supplied to the cathode solution flow path 21 and the anode solution flow path 12, a saturation degree of water in the gas diffusion layer 22A increases, and output reduction occurs due to the diffusibility of gas. By supplying the gas, the saturation degree of water lowers, so that the cell performance is recovered, and the refresh effect is increased. The gas is preferably supplied right after the rinse solution is made to flow, and is preferably supplied at least within five minutes after the finish of supply of the rinse solution. This is because the output reduction is large due to the increase in the saturation degree of water, and if it is assumed that the refresh operation is performed at intervals of an hour, for example, an output during the refresh operation in five minutes is 0 V or significantly small, so that 5/60 of the output is sometimes lost.

When the above refresh operation finishes, the cathode solution is introduced into the cathode solution flow path 21, the anode solution is introduced into the anode solution flow path 12, and CO₂ gas is introduced into the CO₂ gas flow path 23 (S205). Subsequently, the application of the electrolytic voltage between the anode 11 and the cathode 22 performed by the power controller 40 is resumed, to thereby resume the CO₂ electrolysis operation (S206). Note that when the application of the electrolytic voltage is not stopped in S201, the aforementioned resume operation is not performed. For the discharge of the cathode solution and the anode solution from each of the flow paths 12 and 21, gas may be used or the rinse solution may be used.

The supply and flow of the rinse solution (S203) are performed for the purpose of preventing precipitation of an electrolyte contained in the cathode solution and the anode solution, and washing the cathode 22, the anode 11, and each of the flow paths 12 and 21. For this reason, as the rinse solution, water is preferable, water having an electric conductivity of 1 mS/m or less is more preferable, and water having the electric conductivity of 0.1 mS/m or less is still more preferable. In order to remove a precipitate such as the electrolyte in the cathode 22, the anode 11, and the like, an acid rinse solution having a low concentration, of sulfuric acid, nitric acid, hydrochloric acid, or the like may be supplied, and the electrolyte may be dissolved by using the acid rinse solution. When the acid rinse solution having a low concentration is used, a step in which the rinse solution of water is supplied is performed in a step thereafter. It is preferable to perform, right before the gas supply step, the supply step of the rinse solution of water, in order to prevent an additive contained in the rinse solution from remaining. FIG. 1 illustrates the rinse solution supply system 720 having one rinse solution tank 721, but, when a plurality of rinse solutions such as water and the acid rinse solution are used, a plurality of rinse solution tanks 721 corresponding thereto are used.

In particular, for the refresh of the ion-exchange resin, acid or alkaline rinse solution is preferable. This provides an effect of discharging cations or anions substituted in place of protons or OH⁻ in the ion-exchange resin. For this reason, it is preferable that the acid rinse solution and the alkaline rinse solution are made to flow alternately, the rinse solution is combined with water having an electric conductivity of 1 mS/m or less, and gas is supplied between supplies of a plurality of rinse solutions so that the rinse solutions are not mixed.

As the rinse solution, water produced through a reaction may also be used. For example, when CO is produced from CO₂ and protons through reduction, water is generated. It is possible that the water discharged from the cathode 22 at this time is separated through gas/liquid separation, and stored to be used. If it is designed as above, there is no need to newly supply the rinse solution from the outside, which is advantageous in terms of system. Further, by changing an electric potential to increase a reaction current, and increasing an amount of water to be produced, the water may also be supplied to the cathode solution flow path 21. Accordingly, the tank for the produced water, and the pipe, the pump, and the like used for the rinse solution become unnecessary, which provides a configuration that is effective in terms of system. Further, it is also possible that gas containing oxygen is supplied to the cathode solution flow path 21 and a voltage is applied, to thereby perform water decomposition on the electrolytic solution or the rinse solution of the anode 11, and the refresh operation is performed by using water produced by the catalyst from protons or OH⁻ ions moved to a counter electrode. For example, in a case where Nafion is used as an ion exchange membrane in an electrolysis cell in which CO₂ is reduced to CO by using a gold catalyst, when air is flowed through the cathode 22 and an electric potential is applied to the cell to perform water decomposition, protons moved to the cathode 22 are reacted with oxygen by the catalyst, and water is produced. The refresh operation can be performed by using the produced water. Further, it is also possible that hydrogen gas is generated by supplying gas containing no oxygen to the cathode 22 or stopping the supply of gas thereafter, and the generated hydrogen is used to perform the refresh operation to dry the cathode 22. Accordingly, it is also possible to perform the refresh operation of the catalyst by using reducing power of protons and hydrogen.

The gas used for the gas supply and the flow step S204 preferably contains at least one of air, carbon dioxide, oxygen, nitrogen, and argon. Moreover, gas having low chemical reactivity is preferably used. Form such a point, air, nitrogen, and argon are preferably used, and nitrogen and argon are more preferable. The supply of the rinse solution and gas for refresh is not limited only to the cathode solution flow path 21 and the anode solution flow path 12, and in order to wash a surface, of the cathode 22, which is brought into contact with the CO₂ gas flow path 23, the rinse solution and the gas may be supplied to the CO₂ gas flow path 23. It is effective to supply the gas to the CO₂ gas flow path 23 in order to dry the cathode 22 also from the side of the surface which is brought into contact with the CO₂ gas flow path 23.

The above is the description regarding the case where the rinse solution and gas for refresh are supplied to both the anode part 10 and the cathode part 20, but, the rinse solution and gas for refresh may be supplied to only one of the anode part 10 and the cathode part 20. For example, the Faradaic efficiency of the carbon compound varies depending on a contact region between the cathode solution and CO₂ in the gas diffusion layer 22A and the cathode catalyst layer 22B of the cathode 22. In such a case, only by supplying the rinse solution and gas for refresh to only the cathode part 20, the Faradaic efficiency of the carbon compound is sometimes recovered. Depending on a type of the electrolytic solutions (anode solution and cathode solution) to be used, there is sometimes a tendency that precipitation easily occurs in one of the anode part 10 and the cathode part 20. Based on such a tendency of the electrolytic device 1, the rinse solution and gas for refresh may be supplied to only one of the anode part 10 and the cathode part 20. Moreover, depending on an operating time or the like of the electrolytic device 1, the cell performance is sometimes recovered only by drying the anode 11 and the cathode 22. In such a case, it is also possible to supply only the gas for refresh to at least one of the anode part 10 and the cathode part 20. The refresh operation step S105 can be changed in various ways according to an operation condition, a tendency, and the like of the electrolytic device 1.

As described above, in the electrolytic device 1 of the first embodiment, based on whether or not the cell performance of the electrolysis cell 2 satisfies the request criteria, it is determined whether the CO₂ electrolysis operation step S102 is continued or the refresh operation step S105 is performed. By supplying the rinse solution and gas for refresh in the refresh operation step S105, the entry of the cathode solution into the gas diffusion layer 22A, the excess water of the cathode catalyst layer 22B, the deviation of the distribution of the ions and the residual gas in the vicinity of the anode 11 and the cathode 22, the precipitation of the electrolyte in the cathode 22, the anode 11, the anode solution flow path 12, and the cathode solution flow path 21, and the like, which become causes of reducing the cell performance, are removed. Therefore, by resuming the CO₂ electrolysis operation step S102 after the refresh operation step S105, the cell performance of the electrolysis cell 2 can be recovered. By repeating the CO₂ electrolysis operation step S102 and the refresh operation step S105 as above based on the request criteria of the cell performance, it becomes possible to maintain the CO₂ electrolysis performance obtained by the electrolytic device 1 for a long period of time.

Second Embodiment

FIG. 12 is a view illustrating a configuration of a carbon dioxide electrolytic device according to a second embodiment, and FIG. 13 is a sectional view illustrating a configuration of an electrolysis cell in the electrolytic device illustrated in FIG. 12. A carbon dioxide electrolytic device 1X illustrated in FIG. 12 includes an electrolysis cell 2X, an anode solution supply system 100 which supplies an anode solution to the electrolysis cell 2X, a cathode solution supply system 200 which supplies a cathode solution to the electrolysis cell 2X, a gas supply system 300 which supplies carbon dioxide (CO₂) gas to the electrolysis cell 2X, a product collection system 400 which collects a product produced by a reduction reaction in the electrolysis cell 2X, a control system 500 which detects a type and a production amount of the collected product, and performs control of the product and control of a refresh operation, a waste solution collection system 600 which collects a waste solution of the cathode solution and the anode solution, and a refresh material source 700 which recovers an anode, a cathode, or the like of the electrolysis cell 2X, similarly to the carbon dioxide electrolytic device 1 according to the first embodiment.

The carbon dioxide electrolytic device 1X illustrated in FIG. 12 basically includes a configuration similar to that of the electrolytic device 1 illustrated in FIG. 1, except that a configuration of the electrolysis cell 2X is different. As illustrated in FIG. 13, the electrolysis cell 2X includes a reaction tank 53 having an anode solution tank 51, a cathode solution tank 52, and a separator 30 which separates these anode solution tank 51 and cathode solution tank 52. The anode solution tank 51 has a solution inlet port 54A and a solution discharge port 55A connected to the anode solution supply system 100, and a gas inlet port 56A and a gas discharge port 57A. An anode solution is introduced from and discharged to the anode solution supply system 100 to/from the anode solution tank 51. An anode 11 is disposed in the anode solution tank 51 so as to be immersed into the anode solution. The anode 11 is connected to a power controller 40 via a current introduction portion 58A.

The cathode solution tank 52 has a solution inlet port 54B and a solution discharge port 55B connected to the cathode solution supply system 200, and a gas inlet port 56B and a gas discharge port 57B connected to the gas supply system 300. A cathode solution is introduced from and discharged to the cathode solution supply system 200 to/from the cathode solution tank 52. Moreover, CO₂ gas is introduced from the gas supply system 300 into the cathode solution tank 52, and gas containing a gaseous product is sent to the product collection system 400. In order to increase solubility of the CO₂ gas in the cathode solution, the CO₂ gas is preferably released into the cathode solution from the gas inlet port 56B. A cathode 22 is disposed in the cathode solution tank 52 so as to be immersed into the cathode solution. The cathode 22 is connected to the power controller 40 via a current introduction portion 58B.

A gaseous substance supply system 710 of the refresh material source 700 is connected to the gas inlet port 56A of the anode solution tank 51 and the gas inlet port 56B of the cathode solution tank 52 via pipes. A rinse solution supply system 720 of the refresh material source 700 is connected to the solution inlet port 54A of the anode solution tank 51 and the solution inlet port 54B of the cathode solution tank 52 via pipes. The solution discharge port 55A of the anode solution tank 51 and the solution discharge port 55B of the cathode solution tank 52 are connected to the waste solution collection system 600 via pipes. The gas discharge port 57A of the anode solution tank 51 and the gas discharge port 57B of the cathode solution tank 52 are connected to the waste solution collection system 600 via pipes, and gas is recovered into a not-illustrated waste gas collection tank via the waste solution collection system 600 or released into the atmosphere. Composing materials and the like of the respective parts are similar to those of the electrolytic device 1 of the first embodiment, and details thereof are as described above.

In the electrolytic device 1X of the second embodiment, a start-up step S101 of the electrolytic device 1X and a CO₂ electrolysis operation step S102 are performed in a similar manner to the electrolytic device 1 of the first embodiment, except that supply modes of the anode solution, the cathode solution, and the CO₂ gas are different. A determination step S103 regarding whether or not the request criteria of the cell performance are satisfied, is also performed in a similar manner to the electrolytic device 1 of the first embodiment. When it is determined that the cell performance does not satisfy the request criteria, a refresh operation step S105 is performed. In the electrolytic device 1X of the second embodiment, the refresh operation step S105 is performed as follows.

First, a CO₂ reduction reaction is stopped. Next, the anode solution and the cathode solution are discharged from the anode solution tank 51 and the cathode solution tank 52. At this time, application of an electrolytic voltage performed by the power controller 40 may be maintained or stopped. Next, a rinse solution is supplied from the rinse solution supply system 720 to the anode solution tank 51 and the cathode solution tank 52, to thereby wash the anode 11 and the cathode 22. While the rinse solution is supplied, a refresh voltage is applied between the anode 11 and the cathode 22, in a similar manner to the first embodiment. Next, gas is supplied from the gaseous substance supply system 710 to the anode solution tank 51 and the cathode solution tank 52, to thereby dry the anode 11 and the cathode 22. The gas and the rinse solution used for the refresh operation step S105 are similar to those in the first embodiment. When the above refresh operation finishes, the anode solution is introduced into the anode solution tank 51, the cathode solution is introduced into the cathode solution tank 52, and CO₂ gas is supplied into the cathode solution. Subsequently, the CO₂ electrolysis operation is resumed. When the application of the electrolytic voltage performed by the power controller 40 is stopped, the application is resumed. For the discharge of the cathode solution and the anode solution from each of the solution tanks 51 and 52, gas may be used or the rinse solution may be used. However, amounts of the cathode solution and the anode solution are larger than those in the first embodiment. In order to reduce a period of time of the refresh operation, it is preferable that the solutions are discharged by using the gas, and then the rinse solution is supplied.

In the electrolytic device 1X of the second embodiment, the refresh operation may also be performed as follows. The current introduction portions 58 (58A, 58B) provided to an upper portion of the electrolysis cell 2X are detached, and the anode 11 and the cathode 22 are taken outside to be exposed from the anode solution and the cathode solution. Next, the anode 11 and the cathode 22 are immersed into the rinse solution to be washed. While the anode 11 and the cathode 22 are immersed into the rinse solution, a refresh voltage is applied between the anode 11 and the cathode 22, in a similar manner to the first embodiment. Next, the anode 11 and the cathode 22 are taken out from the rinse solution, and dried by blowing gas. Next, the current introduction portions 58 (58A, 58B) are attached, and the anode 11 and the cathode 22 are immersed into the anode solution and the cathode solution. Subsequently, the CO₂ electrolysis operation is resumed. Accordingly, the discharge and the introduction of the anode solution and the cathode solution from/to the anode solution tank 51 and the cathode solution tank 52 are omitted, so that it is possible to reduce a period of time of the refresh operation.

Also in the electrolytic device 1X of the second embodiment, based on whether or not the cell performance of the electrolysis cell 2X satisfies the request criteria, it is determined whether the CO₂ electrolysis operation is continued or the refresh operation is performed. By supplying the rinse solution and the gas in the refresh operation step, deviation of distribution of ions and residual gas in the vicinity of the anode 11 and the cathode 22, which become a cause of reducing the cell performance, is eliminated, and the precipitation of the electrolyte or the like in the anode 11 and the cathode 22 is removed. Therefore, by resuming the CO₂ electrolysis operation after the refresh operation step, the cell performance of the electrolysis cell 2X can be recovered. By repeating the CO₂ electrolysis operation and the refresh operation based on the request criteria of the cell performance, it becomes possible to maintain the CO₂ electrolysis performance obtained by the electrolytic device 1X for a long period of time.

Third Embodiment

FIG. 14 is a view illustrating a configuration of a carbon dioxide electrolytic device according to a third embodiment, and FIG. 15 is a sectional view illustrating a configuration of an electrolysis cell in the electrolytic device illustrated in FIG. 14. A carbon dioxide electrolytic device 1Y illustrated in FIG. 14 includes an electrolysis cell 2Y, an anode solution supply system 100 which supplies an anode solution to the electrolysis cell 2Y, a gas supply system 300 which supplies carbon dioxide (CO₂) gas to the electrolysis cell 2Y, a product collection system 400 which collects a product produced by a reduction reaction in the electrolysis cell 2Y, a control system 500 which detects a type and a production amount of the collected product, and performs control of the product and control of a refresh operation, a waste solution collection system 600 which collects a waste solution of the anode solution, and a refresh material source 700 which recovers an anode, a cathode, or the like of the electrolysis cell 2Y, similarly to the carbon dioxide electrolytic device 1 according to the first embodiment.

The carbon dioxide electrolytic device 1Y illustrated in FIG. 14 basically includes a configuration similar to that of the electrolytic device 1 illustrated in FIG. 1, except that the configuration of the electrolysis cell 2Y is different, and a cathode solution supply system 200 is not included. As illustrated in FIG. 15, the electrolysis cell 2Y includes an anode part 10, a cathode part 20, and a separator 30. The anode part 10 includes an anode 11, an anode solution flow path 12, and an anode current collector 13. The cathode part 20 includes a cathode 22, a CO₂ gas flow path 23, and a cathode current collector 24. A power controller 40 is connected to the anode 11 and the cathode 22 via a current introduction member.

The anode 11 preferably has a first surface 11 a which is brought into contact with the separator 30, and a second surface 11 b which faces the anode solution flow path 12. The first surface 11 a of the anode 11 is brought into close contact with the separator 30. The anode solution flow path 12 is formed of a pit (groove portion/concave portion) provided in a flow path plate 14. The anode solution flows through inside the anode solution flow path 12 so as to be brought into contact with the anode 11. The anode current collector 13 is electrically brought into contact with a surface on a side opposite to the anode 11 of the flow path plate 14 which forms the anode solution flow path 12. The cathode 22 has a first surface 22 a which is brought into contact with the separator 30, and a second surface 22 b which faces the CO₂ gas flow path 23. The CO₂ gas flow path 23 is formed of a pit (groove portion/concave portion) provided in a flow path plate 28. The cathode current collector 24 is electrically brought into contact with a surface on a side opposite to the cathode 22 of the flow path plate 28 which forms the CO₂ gas flow path 23.

A gaseous substance supply system 710 and a rinse solution supply system 720 of the refresh material source 700 are connected to the anode solution flow path 12 and the CO₂ gas flow path 23 via pipes. The anode solution flow path 12 and the CO₂ gas flow path 23 are connected to the waste solution collection system 600 via pipes. A rinse solution discharged from the anode solution flow path 12 and the CO₂ gas flow path is recovered into a waste solution collection tank 601 of the waste solution collection system 600. Gas for refresh discharged from the anode solution flow path 12 and the CO₂ gas flow path is recovered into a not-illustrated waste gas collection tank via the waste solution collection system 600 or released into the atmosphere. Composing materials and the like of the respective parts are similar to those of the electrolytic device 1 of the first embodiment, and details thereof are as described above.

In the electrolytic device 1Y of the third embodiment, a start-up step S101 of the electrolytic device 1Y and a CO₂ electrolysis operation step S102 are performed in a similar manner to the electrolytic device 1 of the first embodiment, except that supply of a cathode solution is not performed. Note that a reduction reaction of CO₂ in the cathode part 20 is performed by CO₂ supplied from the CO₂ gas flow path 23 and the anode solution permeated the cathode 22 via the separator 30. A determination step S103 regarding whether or not the request criteria of the cell performance are satisfied, is also performed in a similar manner to the electrolytic device 1 of the first embodiment. When it is determined that the cell performance does not satisfy the request criteria, a refresh operation step S105 is performed. In the electrolytic device 1Y of the third embodiment, the refresh operation step S105 is performed as follows.

First, a CO₂ reduction reaction is stopped. At this time, application of an electrolytic voltage performed by the power controller 40 may be maintained or stopped. Next, the anode solution is discharged from the anode solution flow path 12. Next, a rinse solution is supplied from the rinse solution supply system 720 to the anode solution flow path 12 and the CO₂ gas flow path 23, to thereby wash the anode 11 and the cathode 22. While the rinse solution is supplied, a refresh voltage is applied between the anode 11 and the cathode 22, in a similar manner to the first embodiment. Next, gas is supplied from the gaseous substance supply system 710 to the anode solution flow path 12 and the CO₂ gas flow path 23, to thereby dry the anode 11 and the cathode 22. The gas and the rinse solution used for the refresh operation step are similar to those in the first embodiment. When the above refresh operation finishes, the anode solution is introduced into the anode solution flow path 12, and CO₂ gas is introduced into the CO₂ gas flow path 23. Subsequently, the CO₂ electrolysis operation is resumed. When the application of the electrolytic voltage performed by the power controller 40 is stopped, the application is resumed.

Also in the electrolytic device 1Y of the third embodiment, based on whether or not the cell performance of the electrolysis cell 2Y satisfies the request criteria, it is determined whether the CO₂ electrolysis operation is continued or the refresh operation is performed. By supplying the rinse solution and the gas in the refresh operation step, deviation of distribution of ions in the vicinity of the anode 11 and the cathode 22, which become a cause of reducing the cell performance, is eliminated, and further, excess water in the cathode 22, the precipitation of the electrolyte in the anode 11 and the cathode 22, blocking of the flow path caused by the precipitation of the electrolyte, and the like are removed. Therefore, by resuming the CO₂ electrolysis operation after the refresh operation step, the cell performance of the electrolysis cell 2Y can be recovered. By repeating the CO₂ electrolysis operation and the refresh operation as above based on the request criteria of the cell performance, it becomes possible to maintain the CO₂ electrolysis performance obtained by the electrolytic device 1Y for a long period of time.

When liquid passes through the separator 30 at a relatively low pressure, for example, a hydrophilic polytetrafluoroethylene (PTFE) porous body or the like is used, the rinse solution is supplied to only the anode solution flow path 12, and a pressure is applied to the liquid at an anode outlet by using a not-illustrated valve or the like or the anode outlet is blocked. Accordingly, the rinse solution passes through the separator 30, flows into the cathode 22, and the rinse solution flows out from a discharge port of the cathode 22. This makes it possible to perform the refresh of the cathode 22 and the refresh of the anode 11 at the same time. This configuration eliminates the necessity of the device which makes the rinse solution flow through the cathode 22, so that the device becomes compact in size, and further, the system is simplified, which is preferable.

Note that a pipe through which air gas is introduced into the cathode 22 may be connected to the cathode 22. At a time of the refresh, it is possible that gas containing air is supplied to the cathode 22, and a refresh voltage is applied between the anode 11 and the cathode 22, to thereby cause a water electrolysis reaction. On the anode 11 side, oxygen is generated by an oxidation catalyst, and generated protons move to the cathode 22 through the separator 30 or an electrolyte membrane. In the cathode 22, the protons and oxygen in the air are reacted by a cathode catalyst, resulting in that water is produced. By using the produced water, salts in the cathode can be dissolved to be discharged. Further, the produced water is pure water, so that it can be used to wash the cathode 22. At this time, impurities in the cathode 22 can be subjected to reduction treatment by using the protons moved to the cathode 22, and it is possible to regenerate the catalyst and the members. This configuration eliminates the necessity of the device which supplies the rinse solution to the cathode 22, so that the device becomes compact in size, and further, the system is simplified, which is preferable. Further, when, before the flow of the CO₂ gas to be performed thereafter, the air flowed through the cathode is stopped, the generated protons react with each other to generate hydrogen, which enables to push out generated water. When the oxygen-containing gas is stopped before performing push with CO₂, a regeneration function of the catalyst and the members provided by the protons becomes more effective. This is because other catalysts which are difficult to be reduced and the respective members of the cathode 22 are reduced, due to the absence of oxygen. Concretely, there can be cited organic matters of impurities, metal oxides, and the like. When CO₂ is supplied thereafter to cause a reaction, it is possible to further expect a refresh effect.

EXAMPLES

Next, examples, comparative examples, and evaluation results thereof will be described.

Examples 1 to 8, Comparative Examples 1, 2

An electrolytic device illustrated in FIG. 14 was fabricated, and an electrolysis performance of carbon dioxide was examined. First, on a carbon paper provided with a porous layer, a cathode to which carbon particles on which gold nanoparticles were supported were applied, was produced by the following procedure. A coating solution in which the carbon particles on which the gold nanoparticles were supported, pure water, a Nafion solution, and ethylene glycol were mixed was produced. An average particle diameter of the gold nanoparticles was 8.7 nm, and a supported amount thereof was 18.9 mass %. The coating solution was filled in an air brush, and spray-coated on the carbon paper provided with the porous layer, by using Ar gas. After the coating, washing was performed by flowing pure water for 30 minutes, and thereafter, the organic matter such as ethylene glycol was oxidized to be removed through immersion in a hydrogen peroxide solution. This was cut into a size of 2×2 cm to be set as the cathode. Note that a coating amount of Au was estimated as about 0.2 mg/cm² from a mixing amount of the gold nanoparticles and the carbon particles in the coating solution. For an anode, an electrode in which IrO₂ nanoparticles to be a catalyst were applied to Ti mesh was used. As the anode, one in which IrO₂/Ti mesh was cut into 2×2 cm was used.

As illustrated in FIG. 2, the electrolysis cell 2 was produced in a manner that the cathode current collector 24, the CO₂ gas flow path 23 (the third flow path plate 28), the cathode 22, the cathode solution flow path 21 (the second flow path plate 25), the separator 30, the anode 11, and the anode solution flow path 12 (the anode current collector 13) were stacked in this order from the top, the stack was sandwiched by the not-illustrated support plates, and tightened by the bolts. For the separator 30, a PTFE porous body (product name: POREFLON, manufactured by Sumitomo Electric Industries, Ltd.) after being subjected to hydrophilic treatment was used. The IrO₂/Ti mesh of the anode 11 was brought into close contact with the PTFE porous body. A thickness of the cathode solution flow path 21 was set to 1 mm. Note that an evaluation temperature was set to room temperature.

The electrolytic device 1 illustrated in FIG. 14 was fabricated using the above-described electrolysis cell 2, and the electrolytic device was operated under the following condition. CO₂ gas was supplied to the CO₂ gas flow path of the electrolysis cell at 60 sccm, and an aqueous potassium hydroxide solution (concentration 1 M KOH) was introduced into the cathode solution flow path at a flow rate of 2 mL/min. Next, by controlling a voltage with the use of the power controller, a voltage of 2.2 V was applied between the anode and the cathode to make a current flow, an electrolytic reaction of CO₂ was caused, and a cell voltage at that time was measured, and collected by the data collection and controller. Further, a part of gas output from the CO₂ gas flow path was collected, and production amounts of CO gas produced by a reduction reaction of CO₂ and H₂ gas produced by a reduction reaction of water were analyzed by a gas chromatograph. In the data collection and controller, based on the gas production amounts, a partial current density of CO or H₂, and Faradaic efficiency being a ratio between the entire current density and the partial current density were calculated and collected.

After 31 minutes from the start of the operation, the refresh operation was performed. In the refresh operation, while supplying distilled water of about 1 cc to the cathode, the refresh operation was performed for about one minute while maintaining the voltage between the anode and the cathode to a value at a time of the electrolysis operation in example 1, and then the CO₂ gas flow rate was increased to 200 ccm. A period of time of increasing the gas flow rate was about 30 seconds. Table 1 presents an entire current density, CO Faradaic efficiency, and H₂ Faradaic efficiency which were collected every about 30 minutes.

In example 2, a reference electrode was disposed at an upstream portion of the anode solution flow path 12. For the reference electrode, Hg/HgO was used. In the refresh operation, distilled water was supplied to the cathode in a similar manner to example 1, when the flow path was filled with the distilled water, an electric potential of the anode was adjusted so that an electric potential of the cathode with respect to the reference electrode became 1.0 V, and the refresh operation was performed for about one minute. After the reaction, the supply of the distilled water was stopped, and the CO₂ gas flow rate was increased to 200 ccm. A period of time of increasing the gas flow rate was about 30 seconds. Table 1 presents an entire current density, CO Faradaic efficiency, and H₂ Faradaic efficiency which were collected every about 30 minutes.

In example 3, the refresh operation was performed under a condition similar to that of example 2, except that the electric potential of the anode was adjusted so that the electric potential of the cathode with respect to the electric potential of the reference electrode became 1.3 V. Table 1 presents an entire current density, CO Faradaic efficiency, and H₂ Faradaic efficiency which were collected every about 30 minutes.

In example 4, the refresh operation was performed under a condition similar to that of example 2, except that the electric potential of the anode was adjusted so that the electric potential of the cathode with respect to the electric potential of the reference electrode became 1.6 V. Table 1 presents an entire current density, CO Faradaic efficiency, and H₂ Faradaic efficiency which were collected every about 30 minutes.

In example 5, the refresh operation was performed under a condition similar to that of example 2, except that the electric potential of the anode was adjusted so that the electric potential of the cathode with respect to the electric potential of the reference electrode became 2.0 V. Table 1 presents an entire current density, CO Faradaic efficiency, and H₂ Faradaic efficiency which were collected every about 30 minutes.

In example 6, the electric potential of the anode was adjusted so that the electric potential of the cathode with respect to the electric potential of the reference electrode was changed from 0 V to 1.6 V at a rate of 100 mV/s, and when the electric potential of the cathode reached 1.6 V, the electric potential of the anode was adjusted so that the electric potential of the cathode was changed at a rate of −100 mV/s. The sweep from 0 V to 1.6 V, and the sweep from 1.6 V to 0 V were repeated three times. The refresh operation was performed under a condition similar to that of example 2 except the above. Table 1 presents an entire current density, CO Faradaic efficiency, and H₂ Faradaic efficiency which were collected every about 30 minutes.

In example 7, the refresh operation was performed under a condition similar to that of example 6, except that the electric potential of the cathode with respect to the reference electrode was changed from −2.0 V to 1.6 V. Table 1 presents an entire current density, CO Faradaic efficiency, and H₂ Faradaic efficiency which were collected every about 30 minutes.

In example 8, distilled water was supplied to only the anode, and a cathode outlet was blocked, to thereby make the distilled water move to the cathode to be discharged from the cathode outlet. Further, the refresh operation was performed under a condition similar to that of example 1 except that the distilled water was supplied for one minute and then the CO₂ flow rate with respect to the cathode was increased. Table 1 presents an entire current density, CO Faradaic efficiency, and H₂ Faradaic efficiency which were collected every about 30 minutes.

In comparative example 1, operation was continuously performed without performing the refresh operation. In comparative example 2, the refresh operation was performed without applying the voltage between the anode and the cathode while supplying the distilled water to the cathode. Table 1 presents an entire current density, CO Faradaic efficiency, and H₂ Faradaic efficiency which were collected every about 30 minutes.

TABLE 1 Operating time 0 30 Right after 60 90 minutes minutes refresh minutes minutes Example 1 Current density (mA/cm²) 220 182 205 183 180 Faradaic efficiency of CO [%] 93 95  96 95 94 Faradaic efficiency of H₂ [%] 1.2 1.8  1.4 1.6 1.7 Example 2 Current density (mA/cm²) 220 182 203 182 178 Faradaic efficiency of CO [%] 93 95  96 95 94 Faradaic efficiency of H₂ [%] 1.2 1.8  1.4 1.6 1.8 Example 3 Current density (mA/cm²) 220 182 206 184 180 Faradaic efficiency of CO [%] 93 95  96 95 94 Faradaic efficiency of H₂ [%] 1.2 1.8  1.4 1.6 1.7 Example 4 Current density (mA/cm²) 220 182 205 182 176 Faradaic efficiency of CO [%] 93 95  96 95 93 Faradaic efficiency of H₂ [%] 1.2 1.8  1.4 1.7 1.9 Example 5 Current density (mA/cm²) 220 182 201 179 175 Faradaic efficiency of CO [%] 93 95  96 95 94 Faradaic efficiency of H₂ [%] 1.2 1.8  1.4 1.6 1.9 Example 6 Current density (mA/cm²) 220 182 207 185 182 Faradaic efficiency of CO [%] 93 95  96 96 95 Faradaic efficiency of H₂ [%] 1.2 1.8  1.4 1.6 1.6 Example 7 Current density (mA/cm²) 220 182 210 187 184 Faradaic efficiency of CO [%] 93 95  98 97 97 Faradaic efficiency of H₂ [%] 1.2 1.8  1.4 1.4 1.5 Example 8 Current density (mA/cm²) 220 182 208 186 185 Faradaic efficiency of CO [%] 93 95  98 96 95 Faradaic efficiency of H₂ [%] 1.2 1.8  1.4 1.4 1.5 Comp. Current density (mA/cm²) 220 182 182(*) 176 172 Example 1 Faradaic efficiency of CO [%] 93 95  94(*) 93 92 Faradaic efficiency of H₂ [%] 1.2 1.8  1.8(*) 2.1 3.5 Comp. Current density (mA/cm²) 220 182 192 173 168 Example 2 Faradaic efficiency of CO [%] 93 95  96 95 94 Faradaic efficiency of H₂ [%] 1.2 1.8  1.4 1.9 2.1 (*)(Refresh is not performed)

As can be understood from Table 1, by performing the refresh operation by applying the voltage between the anode and the cathode while supplying the rinse solution to the cathode, it is possible to improve at least one of the current density, the CO Faradaic efficiency, and the H₂ Faradaic efficiency. This indicates that the cell performance can be maintained for a longer period of time when compared to the prior art.

Note that configurations of the above-described respective embodiments may be each applied in combination, and further may be partially substituted. Herein, while certain embodiments of the present invention have been described, these embodiments have been presented by way of example only, and are not intended to limit the scope of the inventions. Indeed, the novel embodiments described herein may be embodied in a variety of other forms; furthermore, various omissions, substitutions, and changes in the form of the embodiments described herein may be made without departing from the spirit of the inventions. The accompanying claims and their equivalents are intended to cover such forms or modifications as would fall within the scope and spirit of the invention. 

What is claimed is:
 1. A carbon dioxide electrolytic device, comprising: an electrolysis cell including a cathode to reduce carbon dioxide and thus produce a carbon compound, an anode to oxidize water or hydroxide ions and thus produce oxygen, a carbon dioxide source to supply carbon dioxide to the cathode, a solution source to supply an electrolytic solution containing water to at least one selected from the group consisting of the cathode and the anode, and a separator separating the anode and the cathode; a power controller connected to the anode and the cathode and configured to apply a voltage therebetween; a refresh material source including a gas source to supply a gaseous substance to at least one selected from the group consisting of the anode and the cathode, and a solution supply source to supply a rinse solution to at least one selected from the group consisting of the anode and the cathode; and a controller to control the carbon dioxide source, the solution source, the power controller, and the refresh material source in accordance with request criteria of a performance of the cell and thus stop the supply of the carbon dioxide and the electrolytic solution, and apply the voltage therebetween while supplying the rinse solution thereto.
 2. The device according to claim 1, wherein the solution supply source includes a first solution supply source to supply an acid rinse solution thereto, and a second solution supply source to supply water thereto.
 3. The device according to claim 2, wherein the controller is configured to control the refresh material source to supply the rinse solution from the solution supply source and the gaseous substance from the gas source to at least one selected from the group consisting of the cathode and the anode exposed from the electrolytic solution.
 4. The device according to claim 1, further comprising a flow rate controller to be controlled by the controller and thus adjust a flow rate of at least one selected from the group consisting of the rinse solution and the gaseous sub stance.
 5. The device according to claim 1, wherein the gaseous substance contains at least one selected from the group consisting of air, carbon dioxide, oxygen, nitrogen, and argon.
 6. The device according to claim 1, wherein: the carbon dioxide source has a gas flow path through which the carbon dioxide flows to the cathode; and the solution source has a cathode solution flow path through which a cathode solution of the electrolytic solution flows to the cathode, and an anode solution flow path through which an anode solution of the electrolytic solution flows to the anode.
 7. The device according to claim 6, wherein: the anode has a first surface in contact with the separator, and a second surface facing the anode solution flow path so that the anode solution flows from the anode solution flow path to the anode; the cathode has a first surface facing the cathode solution flow path and a second surface facing the gas flow path; and the cathode solution flow path is disposed between the separator and the cathode so that the cathode solution flows to the separator and the cathode.
 8. The device according to claim 1, wherein: the solution source has a cathode solution tank to store a cathode solution of the electrolytic solution into which the cathode is immersed, and an anode solution tank to store an anode solution of the electrolytic solution into which the anode is immersed; and the carbon dioxide source has a carbon dioxide supply system to supply the carbon dioxide to the cathode solution.
 9. The device according to claim 8, wherein: the carbon dioxide source has a gas flow path through which the carbon dioxide flows to the cathode; the solution source has an anode solution flow path through which the anode solution of the electrolytic solution flows to the anode; and the cathode and the anode are disposed on the separator.
 10. The device according to claim 1, wherein the performance is defined by a parameter including at least one selected from the group consisting of a cell voltage of the cell, a cell current of the cell, and Faradaic efficiency of the carbon compound.
 11. The device according to claim 6, wherein the performance is defined by parameters including at least one selected from the group consisting of a cell voltage of the cell, a cell current of the cell, and Faradaic efficiency of the carbon compound, and an internal pressure of at least one selected from the group consisting of the cathode solution flow path and the anode solution flow path.
 12. The device according to claim 11, further comprising a pressure controller to be controlled by the controller and thus adjust the internal pressure of at least one selected from the group consisting of the cathode and anode solution flow paths.
 13. A method of electrolyzing carbon dioxide, comprising: preparing an electrolysis cell having a cathode and an anode; supplying carbon dioxide to the cathode, and supplying an electrolytic solution containing water to at least one selected from the group consisting of the cathode and the anode; applying a first voltage between the anode and the cathode to reduce carbon dioxide and thus produce a carbon compound by the cathode, and to oxidize water or hydroxide ions and thus produce oxygen by the anode; and stopping the supply of the carbon dioxide and the electrolytic solution, and applying the first voltage or a second voltage therebetween while supplying a rinse solution to at least one selected from the group consisting of the cathode, in accordance with request criteria of a performance of the cell.
 14. The method according to claim 13, further comprising: discharging the rinse solution therefrom; and supplying a gaseous substance to at least one selected from the group consisting of the cathode and the anode after the discharge of the rinse solution.
 15. The method according to claim 13, wherein the performance is defined by a parameter including at least one selected from the group consisting of a cell voltage of the cell, a cell current of the cell, Faradaic efficiency of the carbon compound, an internal pressure of a cathode solution flow path through which a cathode solution of the electrolytic solution flows to the cathode, and an internal pressure of an anode solution flow path through which an anode solution of the electrolytic solution flows to the anode. 